Processes for the production of metal oxides

ABSTRACT

Provided are processes for producing metal oxides, including pigmentary TiO 2 . In embodiments, a process for producing a metal oxide comprises combining a metal halide and an oxidant in a liquid phase medium under conditions to oxidize the metal halide in the liquid phase medium to produce a metal oxide therefrom.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application claims priority to U.S. Provisional Patent Application No. 63/135,895 that was filed Jan. 11, 2021, the entire disclosure of which is hereby incorporated by reference.

BACKGROUND

Titanium (IV) oxide, more commonly known as titanium dioxide (TiO₂), is mainly sourced from the naturally occurring titanium iron oxide (iron titanate) ore, ilmenite (FeTiO₃). Titanium dioxide is considered the premium white pigment and is used in paints, plastics, paper, and specialty applications. The current state-of-the-art process is a carbochlorination process (2 FeTiO₃+7 Cl₂+3 C→2TiCl₄+2 FeCl₃+3 CO₂) which produces TiCl₄ and FeCl₃ at 1500 K followed by oxidation of TiCl₄ in oxygen at temperatures ranging from 1500 to 2000 K. In 2020, the global production of TiO₂ from the chloride process was over 4 million metric tons (MTs)/year. In 2020, the average price of TiO₂ was $3,250/MT and is only expected to increase. The global TiO₂ market is expected to exceed $67 Billion by 2025 at a 9% CAGR from 2017 fueled by growing consumption of white pigments in paints and plastics. In order to meet this demand, an additional 100,000 MTs of capacity will be needed annually. This translates to building a new production line every year.

SUMMARY

Provided are processes for producing metal oxides, including pigmentary TiO₂. The processes involve the use of a metal halide (e.g., TiCl₄), an oxidant (e.g., ozone), and mild conditions (e.g., near room temperature). In embodiments, the processes further involve the use of liquid CO₂ as an inert solvent. As demonstrated in the Examples, it has been found that liquid TiCl₄ can be completely oxidized in liquid CO₂ using ozone (TiCl₄+⅔ O₃→TiO₂+2 Cl₂) at temperatures ranging from 273 K to 303 K to produce TiO₂ particles. Prior to the present disclosure, it was not known whether the inorganic compound TiCl₄ would have solubility in liquid CO₂ as well as compatibility with components used in reactors for carrying out the present processes. However, conditions were found in which the TiCl₄ and O₃ have substantially miscibility in liquid CO₂. The by-product chlorine is only partially miscible in the liquid CO₂ and therefore, can be separated from the liquid phase. Experiments in a batch reactor show that TiCl₄ dissolved in liquid CO₂ undergoes reaction with O₃ at 293 K to produce amorphous and crystalline TiO₂ (rutile and anatase) and TiOCl₂ particles. Direct reactions between O₃ and TiCl₄ may also occur. The present processes dramatically decrease the energy required for the TiO₂ oxidation step by 60-80%, lowering the cost of production by 15-25%, and reducing global CO₂ emissions from TiO₂ plants by 25-30% (2 million MT/y). The results also show that this unique ozonation process for producing TiO₂ may also be applied to the production of other metal oxides from metal halides, including those which have applications in catalysis, optoelectronics, and photovoltaics.

In embodiments, a process for producing a metal oxide comprises combining a metal halide and an oxidant in a liquid phase medium under conditions to oxidize the metal halide in the liquid phase medium to produce a metal oxide therefrom.

Other principal features and advantages of the disclosure will become apparent to those skilled in the art upon review of the following drawings, the detailed description, and the appended claims.

DETAILED DESCRIPTION

The present processes involve the oxidative conversion of metal halides to metal oxides in the liquid phase. This is by direct contrast to existing gas phase methods in which the chemical reactions occur in the gas phase. This is also by contrast to methods in which the chemical reactions occur at a gas-solid interface such as in atomic layer deposition. In embodiments, a process of producing a metal oxide according to the present disclosure comprises combining a metal halide and an oxidant in a liquid phase medium. In embodiments, the liquid phase medium is provided by the metal halide in its liquid form. In embodiments, the liquid phase medium comprises CO₂. Conditions are used during the process to induce oxidation of the metal halide to produce the metal oxide.

A variety of metal halides may be used. Generally, however, the metal halide is a liquid and/or is one that is miscible in the liquid phase medium under the conditions being used to induce oxidation. The metal halide may be formed from a single metal or more than one metal (i.e., mixed metal halides are encompassed). The metal of the metal halide may be selected from transition metals, metalloids, etc. Specific metals include Ti, Zr, Sn, Nb, Ta, W, Hf, Ge, V, In, Sb, Mo, Re, Ru, Ni, Fe, Cr, Mn, Al, and combinations thereof. For purposes of the present disclosure, each of these specific metals is considered to be a transition metal or a metalloid. The halide of the metal halide is derived from a halogen, e.g., F, Cl, Br, I. Combinations of different types of metal halides may be used.

A variety of oxidants may be used. Oxidants such as ozone (O₃) and nitrous oxide (N₂O) may be used. Combinations of different types of oxidants may be used. The oxidant may be in its liquid or gaseous state under the conditions being used to induce oxidation. The oxidant may be provided as a mixture, e.g., O₃ in O₂ or O₃ in air. In embodiments, the oxidant is not pure O₂. In embodiments, if O₂ is used, it is combined with another oxidant, e.g., O₃, N₂O.

As noted above, the oxidation conversion of the metal halide to the metal oxide is carried out in the liquid phase. In embodiments, this liquid phase is provided by the liquid phase medium comprising CO₂, which acts as an inert solvent for the metal halide reactant and the oxidant as well as a heat sink for the reaction. As further described below, liquid CO₂ itself is a suitable liquid phase medium, i.e., the liquid phase medium may be pure liquid CO₂. However, other additives may be included in the liquid phase medium. Illustrative additives include a variety of directing agents selected to promote the formation of certain crystalline phases, particle sizes, and/or particle shapes for the metal oxide. Suitable directing agents include, e.g., ZnCl₂, ZnO, MgCl₂, NaCl, and combinations thereof.

In other embodiments, the liquid phase medium may be provided by the metal halide in its liquid form and CO₂ is not necessary. In such embodiments, however, other additives such as directing agents may be included in the liquid phase medium as described above.

Thus, in embodiments, the liquid phase medium consists of the metal halide, and optionally, one or both of CO₂ and a directing agent. These embodiments encompass the selected oxidant(s) being dissolved within the liquid phase medium.

Conditions for inducing oxidation of the metal halide reactant in the liquid phase medium include parameters such as the temperature, the pressure, and the relative amounts of the metal halide, the oxidant, and, if present, CO₂. If CO₂ is used, the temperature and pressure may be selected to liquefy CO₂. They may also be selected to adjust the concentration of the oxidant and the metal halide in the liquid phase medium (e.g., ozone solubilities in liquid CO₂ can be tuned by the appropriate selection of temperature and pressure). Illustrative temperatures of the liquid phase medium include those in the range of from 0° C. to 30° C., from 10° C. to 30° C., from 20° C. to 30° C., and from 20° C. to 25° C. The temperature may be no greater than the critical temperature of CO₂ (about 31.1° C.). This further includes embodiments in which the temperature is no greater than 25° C. These temperatures are orders of magnitude lower than those used in existing carbochlorination processes.

The pressure refers to the total pressure of the vapor phase/dense phase present over the liquid phase medium. Illustrative pressures include those in the range from greater than 1 bar to 100 bar. This includes embodiments in which the pressure is in the range from greater than 1 bar to 95 bar, from greater than 1 bar to 90 bar, from greater than 1 bar to 85 bar, from greater than 1 bar to 80 bar, or from 5 bar to 75 bar. This further includes embodiments in which the pressure is no greater than the critical pressure of CO₂ (about 73.9 bar).

In embodiments, supercritical CO₂ is used, in which the temperature and pressure are greater than the critical temperature and critical pressure of CO₂.

In embodiments in which CO₂ is not used, the temperature and pressure may be within any of the values described above.

The relative amounts of the metal halide, oxidant, and, if present, CO₂ may refer to the amounts added to a reaction cell for containing the liquid phase medium. The term “added” may refer to a one-time addition as in a batch reactor system or a continuous addition per unit time as in a continuous flow reactor system. The metal halide and the oxidant may be added in equivalent molar amounts or an excess of oxidant may be used. For example, the molar ratio (by volume) of (metal halide):(oxidant) may be in a range of from 1:0.667. In embodiments in which CO₂ is present, the molar ratio of the (combined metal halide/oxidant):CO₂ may be in a range of from 1:0.1 to 1:2. If directing agents are used, these may be included in any amount to achieve the desired effect (e.g., desired crystalline phase, particle size, particle shape).

As noted above, the present processes may be carried out in a variety of reactor systems, including batch reactor systems and continuous flow reactor systems.

As noted above, the oxidation reactions of the present processes convert the metal halide reactant to its metal oxide. The metal oxide produced is desirably fully oxidized, but at least in embodiments, partial oxidation products may also be produced. For example, the present processes convert TiCl₄ to TiO₂, but some TiOCl₂ and TiOHCl hydrates may be also be produced. However, the conditions described above may be adjusted to achieve a desired product selectivity/yield, including maximizing the selectivity/yield of the fully oxidized metal oxide product. In embodiments, the yield of the fully oxidized metal oxide product, e.g., TiO₂, is at least 90 weight %, at least 95 weight %, at least 98 weight %, or at least 99 weight %.

The metal oxide product(s) produced by the present processes is generally particulate in form. By “particulate” it is meant that the metal oxide product is in the form of distinct, distinguishable particles, by contrast to a film, layer, or coating of the metal oxide. The particulate morphology may be confirmed using standard imaging techniques, e.g., transmission electron microscopy.

The particles of the metal oxide product may be characterized by their shape and size. The particles may be geometric in shape, but this does not necessarily mean perfectly geometric. Depending upon the use of a particular directing agent, other shapes may be produced. The particles are generally small, having at least one dimension (i.e., 1, 2, or 3) of less than 1000 nm, less than 750 nm, less than 500 nm, less than 300 nm, in a range of from 50 nm to 500 nm or from 100 nm to 300 nm. The term “pigmentary” may be used to describe metal oxide particles having each of their dimensions less than 500 nm, including from 100 nm to 300 nm. The size may be an average size, i.e., an average value as determined from a sample of a plurality of particles. Control of the sizes and distribution of sizes may be facilitated by using a directing agent as described above.

The particles of the metal oxide product may also be characterized by their crystalline phase, control over which may be facilitated by using a directing agent as described above. By way of example, the present processes may be used to convert TiCl₄ to anatase TiO₂, rutile TiO₂, or both.

The present process may include a variety of other steps, e.g., collecting the metal oxide, separating by-product(s), etc.

EXAMPLES Example 1—Miscibility of TiCl₄ in Liquid CO₂

1 mL of TiCl₄ was added inside a N₂ purged dry box using a syringe to a high-pressure view cell with an interior volume of 20 mL. The view cell was sealed and removed from the N₂ drybox. The view cell was connected to a syringe pump filled with liquid CO₂. 10 mL liquid CO₂ was added to the view cell at 20° C. The TiCl₄ liquid was completely miscible in the liquid CO₂.

Example 2—Reaction of TiCl₄ in Liquid CO₂ with O₃

1 mL of TiCl₄ was added inside a N₂ purged dry box using a syringe to a high-pressure view cell with an interior volume of 20 mL. The view cell was sealed and removed from the N₂ drybox. The view cell was connected to a syringe pump filled with liquid CO₂. 10 mL liquid CO₂ was added to the view cell at 20° C. The TiCl₄ liquid was completely miscible in the liquid CO₂. 1 mL of ozone was added to the view cell. The pressure used was about 57 bar. The liquid CO₂ turned the expected purple color upon addition of the ozone. Slowly over about 30 seconds the solution began to become turbid. The turbidity was the initial formation of TiO₂. After 30 minutes it was clear that particles of TiO₂ were forming on the surfaces (windows and walls) of the view cell. After 60 minutes all the ozone had been consumed (purple color dissipated) and a white powder was observed inside the view cell on the walls and windows. The solution had a slight yellow/green tint indicating evidence of Cl₂ or Cl containing materials. The CO₂ was slowly vented from the view cell and the view cell was purged with N₂ to prevent any air/water vapor from entering the view cell. The view cell was disassembled and a white powder had formed on the walls and windows of the view cell. X-ray diffraction (XRD) analysis of the powder found TiO₂ (anatase and rutile) with minor amounts of TiOCl₂ and TiOHCl hydrates. The TiOCl₂ and TiOHCl hydrates were the result of excess TiCl₄ remaining in the view cell upon exposure to air containing water vapor while evaporating the CO₂ (e.g., TiCl₄+H₂O->TiOCl₂+2HCl).

Example 3—Reaction of TiCl₄ in Liquid CO₂ with Excess O₃

The view cell was thoroughly cleaned with acetone to remove any water contamination on the surfaces and allowed to dry inside a N₂ purged dry box. 0.25 mL of TiCl₄ was added inside a N₂ purged dry box using a syringe to a high-pressure view cell with an interior volume of 20 mL. The view cell was sealed and removed from the N₂ drybox. The view cell was connected to a syringe pump filled with liquid CO₂. 10 mL liquid CO₂ was added to the view cell at 20° C. The TiCl₄ liquid was completely miscible in the liquid CO₂. 1 mL of ozone was added to the view cell. The pressure used was about 57 bar. The liquid CO₂ turned the expected purple color upon addition of the ozone. Slowly over about 30 seconds the solution began to become turbid. The turbidity was the initial formation of TiO₂. After 30 minutes it was clear that particles of TiO₂ were forming on the surfaces (windows and walls) of the view cell. After 60 minutes all the ozone had been consumed (purple color dissipated) and a white powder was observed inside the view cell on the walls and windows. The solution had a slight yellow/green tint indicating evidence of Cl₂ or Cl containing materials. The CO₂ was slowly vented from the view cell and the view cell was purged with N₂ to prevent any air/water vapor from entering the view cell. The view cell was disassembled and a white powder had formed on the walls and windows of the view cell that were below the liquid CO₂ level. Some yellow deposits had formed above the liquid CO₂ level. X-ray diffraction (XRD) analysis of the white powder found TiO₂ (anatase and rutile). The yellow powder was TiOCl₂ and TiOHCl hydrates as a result of excess TiCl₄ remaining in the view cell upon exposure to air containing water vapor while evaporating the CO₂ (e.g., TiCl₄+H₂O->TiOCl₂+2HCl).

The word “illustrative” is used herein to mean serving as an example, instance, or illustration. Any aspect or design described herein as “illustrative” is not necessarily to be construed as preferred or advantageous over other aspects or designs. Further, for the purposes of this disclosure and unless otherwise specified, “a” or “an” means “one or more.”

If not already included, all numeric values of parameters in the present disclosure are proceeded by the term “about” which means approximately. This encompasses those variations inherent to the measurement of the relevant parameter as understood by those of ordinary skill in the art. This also encompasses the exact value of the disclosed numeric value and values that round to the disclosed numeric value.

The foregoing description of illustrative embodiments of the disclosure has been presented for purposes of illustration and of description. It is not intended to be exhaustive or to limit the disclosure to the precise form disclosed, and modifications and variations are possible in light of the above teachings or may be acquired from practice of the disclosure. The embodiments were chosen and described in order to explain the principles of the disclosure and as practical applications of the disclosure to enable one skilled in the art to utilize the disclosure in various embodiments and with various modifications as suited to the particular use contemplated. It is intended that the scope of the disclosure be defined by the claims appended hereto and their equivalents. 

What is claimed is:
 1. A process for producing a metal oxide, the process comprising combining a metal halide and an oxidant in a liquid phase medium under conditions to oxidize the metal halide in the liquid phase medium to produce a metal oxide therefrom.
 2. The process of claim 1, wherein the metal halide is a liquid under the conditions being used in the process.
 3. The process of claim 1, wherein the metal halide is a metal chloride.
 4. The process of claim 1, wherein the metal of the metal halide is selected from the group consisting of transition metals, metalloids, and combinations thereof.
 5. The process of claim 4, wherein the metal of the metal halide is selected from the group consisting of Ti, Zr, Sn, Nb, Ta, W, Hf, Ge, V, In, Sb, Mo, Re, Ru, Ni, Fe, Cr, Mn, Al, and combinations thereof.
 6. The process of claim 1, wherein the oxidant is ozone.
 7. The process of claim 6, wherein the ozone is combined with oxygen or air.
 8. The process of claim 1, wherein the liquid phase medium comprises CO₂.
 9. The process of claim 8, wherein the CO₂ is liquid CO₂ under the conditions being used in the process.
 10. The process of claim 1, wherein the process is carried out at a temperature and pressure selected to liquefy CO₂.
 11. The process of claim 1, wherein the combining is carried out in the presence of supercritical CO₂.
 12. The process of claim 1, wherein the conditions comprise use of a temperature of no greater than 32° C. and a pressure of greater than 1 bar.
 13. The process of claim 12, wherein the temperature is in a range of from 0° C. to 32° C. and the pressure is in a range of from greater than 1 bar to 100 bar.
 14. The process of claim 1, wherein the liquid phase medium further comprises a directing agent.
 15. The process of claim 1, wherein the metal oxide is a fully oxidized metal oxide.
 16. The process of claim 1, wherein the metal oxide is particulate in form.
 17. The process of claim 16, wherein the metal oxide is pigmentary metal oxide.
 18. The process of claim 1, wherein the metal of the metal halide is titanium, the liquid phase medium comprises CO₂, and the oxidant is ozone.
 19. The process of claim 18, wherein the metal halide is titanium chloride.
 20. The process of claim 19, wherein the CO₂ is liquid CO₂. 